CN103449699B - Device and method for realizing continuous pyrohydrolysis treatment of organic material - Google Patents
Device and method for realizing continuous pyrohydrolysis treatment of organic material Download PDFInfo
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Abstract
The invention discloses a device and a method for realizing continuous pyrohydrolysis treatment of an organic material. According to the method, the organic material is preheated to below 100 DEG C by utilizing flash-off steam, the temperature and the pressure in a booster jar are increased with the flash-off steam, reactants after boosting enter a two-stage reaction unit with tubular mixing heat exchange and pyrohydrolysis reaction, heat fully exchanges with high-temperature and high-pressure steam to perform pyrohydrolysis reaction, one-stage flash-off and two-stage flash-off are continuously performed on the material after reaction, the produced flash-off steam enters the booster jar and a preheating tank respectively as preheating mediums, and the reactants after the flash-off are thrown into a digestion tank after cooling mixing for fermentation to produce marsh gas or directly drying compost. The device comprises the preheating tank, a two-stage continuous pyrohydrolysis reactor consisting of a tubular mixing heat exchanger and a continuous reaction tank, and a flash-off cooling part. The device and the method fully realize the cascade efficient utilization of the system waste heat; compared with the traditional sequencing batch reaction technology, the equipment and the running control of the equipment are simplified, and the continuous pyrohydrolysis reaction of the organic material is realized.
Description
Technical field
The present invention relates to organic thermal hydrolysis technology, particularly relate to a kind of organic continuous thermal hydrolysis treatment unit and method.
Background technology
Along with the development of Chinese national economy, all sharp increases of the organic solid castoff such as mud and changing food waste generation.The organic main treatment process adopting " preheating-anaerobic digestion-dehydration and drying " such as current excess sludge, but this traditional treatment process exists shortcomings such as digestion rate is low, gas production rate is little, digestion period long (residence time reaches 20-30 days).
Thermal hydrolysis digestion process technique is a kind for the treatment of technology mud being carried out to minimizing, resource utilization, stabilization and safe.Thermal hydrolysis reactor is core and the key equipment of sludge hot hydrolysis-anaerobic digester system, and it not only decides the biogas effect of output, and decides the energy consumption of whole sludge treatment equipment.Existing thermal hydrolysis reaction unit and technique can be summarized as two kinds generally: a kind of is adopt the sequence batch mode with active power energy consumption, such as there is the autoclave of alr mode, which can guarantor unit's time larger treatment capacity, but which power consumption is large, the mode that sequence is criticized is strong not to the change adaptability for the treatment of capacity, Controlling System is loaded down with trivial details; Another kind is tubular type continuous thermal hydrolysis reactor.This continuous pipe type processing mode is carried out due to preheating, Hybrid Heating, heat-insulation pressure keeping and flash cooling in same pipe, though can realize continuously, shortcoming one be treatment capacity when increasing reaction tubes size increase, heat transfer effect is affected; Two is without flash vaporization process, so Energy harvesting is unreasonable, three is higher to initial feed concentration requirement.
To sum up, there is the unit time or the problem such as unit energy consumption heat exchange efficiency is lower, the thermal hydrolysis cycle is longer, observable index is larger in the organic thermal hydrolysis such as existing mud fermentative processing technology.
Summary of the invention
Patent of the present invention is for above problem, and object is to provide a kind of passive type continuous thermal hydrolysis system, it is characterized in that except conveying equipment (as: pump), without extra power energy consumption.
In addition, the object of the present invention is to provide a kind of for continuous hot water analytical system, it is characterized in that the dry substance concentration of organic (such as mud) raw material of process can be any concentration within the scope of the output mud mass dryness fraction of sewage work, such as 10%, 15%, 20% etc.
In addition, the object of the present invention is to provide a kind of for continuous hot water analytical system, it is characterized in that the treatment capacity processing organic (such as mud) raw material can flexible.
In the context of the present invention, " tubular-mix heat exchange and thermal hydrolysis reaction two-stage " is interpreted as such process unit: react two subprocess by the heat-insulation pressure keeping after the pyrohydrolysis process of reactant is divided into mixing contact heat-exchanging and reaching predetermined pressure and temperature of reactant and high-temperature high-pressure steam, and these two processes are combined and completed respectively by tubular-mix interchanger and heat-insulation pressure keeping retort.
In the context of the present invention, " passive type continuous thermal hydrolysis " is interpreted as, and in whole thermal hydrolysis system except the pump transported working medium, does not carry out the wasted work for the purpose of enhanced heat exchange such as mix and blend to material.
For achieving the above object, a kind of device for organic continuous thermal hydrolysis that the present invention proposes is:
A kind of organic continuous thermal hydrolysis treatment unit comprises the flash-off steam of employing from successive flash vaporization temperature reducing unit carries out preheating preheating unit to organic matter material, adopt the continuous thermal hydrolysis reaction member of laser heating and thermal hydrolysis reaction, the step flash distillation that after thermal hydrolysis reaction, High Temperature High Pressure organic matter carries out successively and temperature reducing unit; Continuous thermal hydrolysis reaction member comprises one or more and adopts pipe method to make the tube mixer of outside input steam and described organic matter material heat exchange, the heat-insulation pressure keeping thermal hydrolysis retort of one or more parallel connections, the flash tank for carrying out flash distillation to the organic matter obtained through thermal hydrolysis of one or more series connection.Wherein,
Each thermal hydrolysis reaction member comprises the combination of one or more tube mixer and continuous thermal hydrolysis retort, tube mixer has one or more material inlet, one or more high temperature and high pressure steam entrance, each tube mixer has the steam inlet that one or more vapor-nozzle is connected with the physical construction preventing reactant from pouring in down a chimney, and each tube mixer can horizontal or vertical or installation of tilting.Wherein,
The vapor-nozzle of tube mixer also can be the straight pipeline that caliber is significantly less than mixing duct; The physical construction preventing reactant from pouring in down a chimney can adopt check valve to replace, and each steam inlet also can have the inclination installation of tube mixer axis component perpendicular to tube mixer axis.
Each thermal hydrolysis retort has one or more opening for feed, and top has one or more vapour outlet, has one or more Discharge outlet.The thermal hydrolysis retort of described heat-insulation pressure keeping, following rule is followed: the material residence time wherein equals the default thermal hydrolysis reaction times between the distance of opening for feed and discharge port and feeding rate, between 20-60 minute, such as 30 minutes, 40 minutes, 60 minutes; The thermal hydrolysis retort of described heat-insulation pressure keeping, can vertically, level or have simultaneously level and vertical component inclination install.
In order to achieve the above object, the second technical scheme that the present invention proposes is:
Realize a method for organic continuous thermal hydrolysis process, comprise the steps:
Step 1: described organic reactant is supplied continuously the preheating can in preheating unit, under the heating of system two-stage flash steam, is heated to lower than 100 degree of non-boiling states;
Step 2: the reactant after preheating supplies booster jar continuously, under the heating of system level flash-off steam, heats the intermediate pressure be pressurized between normal pressure to thermal hydrolysis reaction pressure;
Step 3: heat the reactant supplying hot water solution reaction member after supercharging, in the tubular-mix heat exchange area of thermal hydrolysis successive reaction unit, the abundant heat exchange of reactant that high temperature and high pressure steam and booster jar are discharged, reach and a little more than preset reaction pressure and temperature;
Step 4: reactant enters retort after mixed heat transfer from tubular-mix interchanger, slowly moves in retort, to retort Discharge outlet;
Step 5: the reactant of discharging from retort outlet enters the flash distillation decrease temperature and pressure stage, through primary flash, make material pressure be reduced to intermediate pressure between reaction pressure and normal pressure, this process discharges the booster jar that flash-off steam enters preheating unit, and carries out temperature-pressure to reactant;
Step 6: the reactant after primary flash enters the two-stage flash stage, about reactant pressures is reduced to normal pressure in this process, temperature is reduced to temperature of saturation corresponding to described pressure, the flash-off steam that this process is discharged enters the low-temperature prewarming tank of preheating unit, and carries out preheating to reaction mass;
Step 7: the reactant after two-stage flash enters Digestive system dilution or interchanger temperature-fall period, and discharges thermal hydrolysis system; Complete the reactant after thermal hydrolysis and can be used for anaerobically fermenting or mummification compost etc.
To sum up, the present invention has the following advantages:
One of advantage of the present invention is, by the combination of tubular heat exchanger and heat-insulation pressure keeping thermal hydrolysis retort, not only realizes pyrohydrolysis process and carries out continuously, and conveniently can regulate the processing load of reactant.
Another advantage of the present invention is, make use of the waste heat of system rationally and effectively, and such as reactant carries out step flash distillation cooling after completing thermal hydrolysis reaction, and preheating flash-off steam is respectively used to reactant and supercharging.
An advantage more of the present invention is, thermal hydrolysis reaction power consumption is few, and such as, thermal hydrolysis reaction process is without any need for the active wasted work for the purpose of enhanced heat exchange.
Other advantages of the present invention, target and feature will be set forth to a certain extent in the following description, and to a certain extent, based on will be apparent to those skilled in the art to contextual investigating, or can be instructed from the practice of the present invention.Target of the present invention and other advantages can be realized by structure specifically noted in specification sheets below and accompanying drawing and be obtained.
Accompanying drawing explanation
Fig. 1 is the composition structural representation of the apparatus and method of a kind of organic continuous thermal hydrolysis process of the present invention.
Fig. 2 is the pipe mixing device structural representation of continuous thermal hydrolysis reaction member in the device of a kind of organic continuous thermal hydrolysis process of the present invention.
Fig. 3 is the pipe mixing device structural representation in another embodiment of continuous thermal hydrolysis reaction member in the device of a kind of organic continuous thermal hydrolysis process of the present invention.
Fig. 4 is the heat-insulation pressure keeping retort structural representation of continuous thermal hydrolysis reaction member in the device of a kind of organic continuous thermal hydrolysis process of the present invention.
Embodiment
For making the object, technical solutions and advantages of the present invention clearly, the present invention is described in further detail below in conjunction with the accompanying drawings and the specific embodiments.
In one embodiment, as shown in Figure 1, the organic reactant 10 with certain dry substance concentration through pump delivery in preheating can 1, the flash-off steam 22 of discharging with two-stage flash tank 6 mixes and heats up, extremely lower than the non-boiling state of 100 degree, be delivered in tubular-mix interchanger 11 by pump 7 bottom preheating can, afterheat steam 20 mixed heat transfer that the flash-off steam 21 of discharging with primary flash tank 5 in 11 and retort 4 are discharged, reactant after pressure and temperature raises all to some extent enters in booster jar 2, after heating supercharging, reactant 12 is delivered to thermal hydrolysis reaction member by pump 9, first enter in tubular-mix interchanger 3, with high-temperature high-pressure steam 27 fully mixed heat transfer, export at tubular-mix interchanger 3 and reach and input in heat-insulation pressure keeping thermal hydrolysis retort 4 slightly above the reaction pressure preset and the reactant 14 of temperature, reactant slowly rises from bottom to top in thermal hydrolysis retort 4, and concurrent heat-dissipating hydrolysis reaction, through certain reaction times, such as 20-60 minute, reactant arrives the reactant outlet 15 of retort 4, completes thermal hydrolysis reaction, completes the reacted reactant of thermal hydrolysis and enter in primary flash tank 5, in primary flash tank, keep certain the stable intermediate pressure between reaction pressure and normal pressure, such as, 0.2-0.6MPa, reactant decrease temperature and pressure, releases flash-off steam 21 simultaneously, reactant 16 after primary flash tank decrease temperature and pressure continues to enter in two-stage flash tank 6, by the effect of pressure relief valve, two-stage flash tank 6 has normal pressure or the steady pressure a little more than normal pressure, and reactant is in primary flash tank 6, decrease temperature and pressure, releases flash-off steam 22 simultaneously, this flash-off steam 22 enters in separating tank 24 with the escaping air 23 of discharging from booster jar top, reactant 17 after decrease temperature and pressure discharges flash tank, with dilution water or with from fermented liquid 18 hybrid cooling in digester to moderate temperature, such as 45-60 degree, so far, reactant 19 completes thermal hydrolysis reaction and Pressure Drop is low to moderate normal pressure, temperature is reduced to moderate temperature, discharges thermal hydrolysis pretreatment system involved in the present invention, enters the last handling processes such as digester fermentation or dehydration and drying compost.
The present embodiment is in concrete enforcement, the flash-off steam 22 of discharging from two-stage flash tank enters separating tank 24 with the escaping air 23 of discharging from booster jar top, separate flash distillation and the liquid state of taking out of and solid matter (organic or condensed water), the dry saturated vapour 25 of discharging from separating tank enters preheating reactant preheating can, and this separator can adopt cyclonic separator or trap.
The present embodiment is in concrete enforcement, for strengthening the heat transfer effect of booster jar 2, after upper and lower temperature difference exceedes certain set(ting)value, can consider to adopt recycle pump 8 to promote that in tank body, temperature of charge reaches even, or adopt the various forms traverse baffle being applicable to tank interior enhanced heat exchange.
The present embodiment is in concrete enforcement, external high temperature high pressure steam 13 is divided into two branch roads after entering this thermal hydrolysis system, namely 26 and 27, wherein the effect of steam 26 is: when system initial launch, tubular-mix interchanger 11 is without steam source, and now steam 26 is for providing initial heating working medium, once produce normal flash-off steam flow in pipeline 20 and 21, then steam-pipe 26 is closed, and no longer provides high temperature and high pressure steam to tubular-mix interchanger 11.
Below in conjunction with Fig. 2, tube mixer apparatus structure described in patent of the present invention and mode of operation are described.
As shown in Figure 2, the described tubular-mix apparatus major function of the present embodiment has been abundant mixed heat transfer that is organic and high-temperature high-pressure steam.Specifically comprise mixing section 33 and heat exchanging segment 34, mixing section 33 outer wall has one or more steam inlet nozzle 32, as shown in A-A section in Fig. 2, vapor-nozzle can be one or more on a certain pipeline section, because described tube mixer operating pressure is higher, generally between 0.6-1MPa, therefore consider the problem of tube wall bearing resistance, multiple nozzle can Heterogeneous Permutation, namely reduces the impact of section stress by reducing vapor-nozzle density on each cross-section of pipeline and number.In addition, nozzle 37 (38) outside should connect vacuum breaker (or other devices preventing organic matter from pouring in down a chimney), and when reducing to prevent vapor pressure, in pipe, organic matter pours in down a chimney in steam-pipe.Described tube mixer mixing section 33 and heat exchanging segment 34, by Flange joint, wherein, consider that high pressure steam enters tube mixer, can produce vibration, therefore mixing section 33 should be taked glissando.
The bonding position of the tube mixer vapor-nozzle described in patent of the present invention and mixing tank main pipeline can be perpendicular to main pipeline central shaft, also can have working medium in mixing tank main pipeline and flow to the vergence direction of component.
The principle of work of the present embodiment tubular-mix apparatus is as follows: as shown in Figure 2, reactant enters tubular-mix interchanger from 31, mix at mixing section 33 with the high temperature and high pressure steam entering tubular-mix interchanger from vapor-nozzle 32 (one or more), in the structure that steam inlet nozzle 32 outer setting prevents mud from pouring in down a chimney, as vacuum breaker.Reactant and steam enter heat exchanging segment 34 along pipeline subsequently, and at heat exchanging segment inner edge flow forward limit mixed heat transfer, at tubular-mix heat exchanger exit 36, reach abundant mixing, temperature reaches unanimity, and enter heat-insulation pressure keeping retort (device 4 in Fig. 1).
For treatment capacity 30t/h, the mixing section latus rectum of the present embodiment is at 150-200mm, and length is advisable at 500-1000mm, and jet exit latus rectum evenly misplaces at 10-15mm, 5-10 and is arranged in mixing section.Heat exchanging segment 34 length is advisable at 1000-2000mm.In the pipe arranging static state/dynamic mixer in heat exchanging segment pipe, insert mixing device is useful for abundant heat exchange.
In addition, illustrate in a particular embodiment below in conjunction with Fig. 3, describe the another kind of alternative structure of tube mixer of the present invention and mode of operation thereof:
As shown in Figure 3, this tube mixer embodiment has mixing section 138 and heat exchanging segment 135 equally, unlike mixing section, there is one or more steam-in 140, first steam enter in jacket structured 134 of mixing section, major part steam enters the mixing section 132 of tube mixer by the import 139 on the relative inner pipe wall of steam-in pipeline, import 139 has the blade of 132 foldings in pipe, under tube mixer normal operation, this blade and inner reaction tube logistics are in the angle being less than 90 degree, such as 30 degree, 45 degree, 60 degree.When vapor pressure reduces, this blade automatically closes under the promotion of inner reaction tube thing, prevents reactant from pouring in down a chimney in steam-pipe.Some steam enters mixing section by the multiple steam holes 133 on inner pipe wall in chuck, reactant mixes on pipe inner edge flowing limit with the steam entering mixing section, enter heat exchanging segment 137 subsequently, at tubular-mix heat exchanger exit 36, reach abundant mixing, reach unanimity along duct orientation temperature, the reactant after mixed heat transfer enters heat-insulation pressure keeping retort.
In a particular embodiment, the tubular-mix interchanger described in patent of the present invention, in the pipe arranging static state/dynamic pipeling mixing tank in its pipe, the abundant mixed heat transfer of insert hybrid element to reactant and steam is useful.
In a particular embodiment, tubular-mix interchanger described in patent of the present invention has steam jacket, namely steam enters pipe sandwich from import 140, the inner tubal wall of interlayer has ventilating pit 133, steam enters interior pipe by these ventilating pits and mixes with reactant, can will arrange the physical construction preventing reactant from pouring in down a chimney at 139 places as above inside described ventilating pit.
The heat-insulation pressure keeping retort of the thermal hydrolysis unit described in patent of the present invention is described below in conjunction with Fig. 4.
Reactant after the abundant heating and pressurizing of foregoing tubular-mix interchanger 44 enters thermal hydrolysis retort bottom heat-insulation pressure keeping retort, traverse baffle 43 is provided with the heat exchange of further intensified response thing and steam in thermal hydrolysis retort, absorb in tubular heat exchanger remaining not by steam that reactant absorbs, along with the increase entering tank body reactant, in tank, reactant is along traverse baffle, slowly even up along tank body further, issue heat-dissipating hydrolysis reaction at the pressure and temperature that tank body is stable simultaneously, final arrival reactant outlet 46, liquid level 48 should export a little more than reactant, complete the reactant 45 of thermal hydrolysis reaction, enter primary flash tank and carry out flash distillation decrease temperature and pressure unit.
Heat-insulation pressure keeping thermal hydrolysis retort of the present invention relies on the effect of bottom inlet reactant thermodynamic state (temperature and pressure) and tank body top controlling valve, thermal hydrolysis retort inside is made to keep stable pressure and temperature, the thermal hydrolysis reaction pressure that this pressure and temperature is desired just and temperature, such as 0.7MPa, 165 degree, such as 0.6MPa, 158.8 degree, easily recognize, at described thermal hydrolysis reacting tank body higher than in the space 42 of discharge gate, the saturation steam had under this pressure exists, when quantity of steam increases, cause described retort top pressure a certain amount of higher than reaction pressure, then retort top controlling valve is opened automatically, steam enters in booster jar from pipeline 41, otherwise if pressure is lower than setting pressure, then this controlling valve is closed automatically.
Heat-insulation pressure keeping thermal hydrolysis retort of the present invention, is connected with the tubular-mix interchanger of multiple parallel connection, regulates thermal hydrolysis treatment capacity easily with the number by switch in parallel tubular reactor in the embodiment of majority.
Heat-insulation pressure keeping thermal hydrolysis retort of the present invention, has the reactant outlet of multiple different heights (horizontal direction) position, as 46 in Fig. 4,47, to adapt to the change of thermal hydrolysis treatment capacity in the embodiment of majority.Such as, in one embodiment, if reacting tank body is vertically placed, when thermal hydrolysis treatment capacity reduces, then should choose the outlet of vertical direction low level as discharge gate, close other discharge ports.
Heat-insulation pressure keeping thermal hydrolysis retort of the present invention, the position of the vertical direction discharge gate corresponding with multiple treatment capacity should be determined according to following condition:
H＝(t×m/ρ)/A
Wherein,
H: represent count from tank base useful volume place along reactant flow in retort to the distance to retort discharge gate, such as in one embodiment, if retort is the tank body that vertical direction is installed, as shown in Figure 4, H is the height vertically that tank base free area place starts.Wherein,
Described free area is in the tank body of nonuniform section area, is the extreme lower position of average cross-section A from tank base conversion, unit: m.
T: the thermal hydrolysis reaction times representing setting. in the embodiment of majority, this time is between 0.3-1 hour.Such as, be 0.5 hour in a particular embodiment, 0.6 hour, unit: hour.
M: represent that reactant imports and exports flow, unit: m at the reactant of thermal hydrolysis retort
3/ hour.
ρ: represent organic reactant density, unit: kg/m
3.
A: the heat-insulation pressure keeping thermal hydrolysis retort described in expression along the sectional area in reagent flow direction, unit: m
2.
In sum, these are only preferred embodiment of the present invention, be not intended to limit protection scope of the present invention.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (6)
1. organic matter material is carried out to a method for continuous thermal hydrolysis, is carried out continuously by following steps:
Step 1: described organic reactant is supplied continuously the preheating can in preheating unit, under the heating of system two-stage flash steam, is heated to lower than 100 degree of non-boiling states;
Step 2: the reactant after preheating supplies booster jar continuously, under the heating of system level flash-off steam, heats the intermediate pressure be pressurized between normal pressure to thermal hydrolysis reaction pressure;
Step 3: heat the reactant supplying hot water solution reaction member after supercharging, in the tubular-mix heat exchange area of thermal hydrolysis successive reaction unit, the abundant heat exchange of reactant that high temperature and high pressure steam and booster jar are discharged, reach and a little more than preset thermal hydrolysis reaction pressure and temperature;
Step 4: reactant enters retort after heat exchange from tubular-mix interchanger, slowly moves in retort, to retort outlet, for a small amount of high pressure steam that maintenance retort stablizes reaction pressure and discharge enters booster jar, to heating organic in booster jar;
Step 5: the reactant of discharging from retort outlet enters the flash distillation decrease temperature and pressure stage, through primary flash, make material pressure be reduced to intermediate pressure between reaction pressure and normal pressure, this process is discharged the supercharging that flash-off steam enters preheating unit and is heated region, and carries out temperature-pressure to reactant;
Step 6: the reactant after primary flash enters the two-stage flash stage, reactant pressures is reduced to normal pressure in this process, temperature is reduced to temperature of saturation corresponding to described reactant pressures, the flash-off steam that this process is discharged enters the preheated zone of preheating unit, and carries out preheating to reaction mass;
Step 7: the reactant after two-stage flash enters Digestive system dilution cooling or interchanger temperature-fall period, discharges thermal hydrolysis system afterwards;
Step 8: complete the reactant after thermal hydrolysis for anaerobically fermenting or the aftertreatment of mummification compost.
2. according to method according to claim 1, it is characterized in that, the device of step 2,3 and 4 correspondences: booster jar, tubular-mix interchanger and thermal hydrolysis retort keep the pressure and temperature of each self stabilization respectively in whole successive reaction.
3. adopt the method for as claimed in claim 1 carrying out continuous thermal hydrolysis to organic matter material organic matter material to be carried out to a device for continuous thermal hydrolysis process, it is characterized in that,
Described thermal hydrolysis treatment unit comprises the flash-off steam of employing from successive flash vaporization temperature reducing unit carries out preheating preheating unit to organic-biological raw material, adopt the continuous thermal hydrolysis reaction member of continuous mixed heat transfer and thermal hydrolysis reaction, the step flash distillation that after thermal hydrolysis reaction, High Temperature High Pressure organic-biological matter is carried out successively and temperature reducing unit;
Continuous thermal hydrolysis reaction member comprises one or more and adopts pipe method to make the tubular-mix interchanger of outside input steam and described organic matter material heat exchange, the thermal hydrolysis retort of the heat-insulation pressure keeping of one or more parallel connections, the flash tank for carrying out flash distillation to the organic matter obtained through thermal hydrolysis of multiple series connection, wherein, each thermal hydrolysis reaction member comprises the combination of one or more tubular-mix interchanger and continuous thermal hydrolysis retort, tubular-mix interchanger has one or more material inlet, one or more high temperature and high pressure steam entrance, each tubular-mix interchanger steam enters reactant pipeline and mixed heat transfer with it by one or more vapor-nozzle, each tubular-mix interchanger can horizontal or vertical or tilt install,
Each thermal hydrolysis retort has one or more opening for feed, and top has one or more vapour outlet, has one or more Discharge outlet.
4. device according to claim 3, it is characterized in that, the described opening for feed of thermal hydrolysis retort and there is following rule between the distance of discharge port and feeding rate: the material residence time wherein equals the default thermal hydrolysis reaction times, between 20-60 minute.
5. device according to claim 4, is characterized in that, the described default thermal hydrolysis reaction times is 30 minutes, 40 minutes or 60 minutes.
6. the device according to any one of claim 3-5, is characterized in that, described thermal hydrolysis retort can vertically, level or tilt install.
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| CN106698870A (en) * | 2015-07-24 | 2017-05-24 | 科尼兹环保科技（大连）有限公司 | Continuous recycling treatment process of sludge |
| CN108015098A (en) * | 2017-12-27 | 2018-05-11 | 郑州凯山生化工程有限公司 | A kind of domestic garbage resource processing method |
| CN110510840A (en) * | 2018-05-21 | 2019-11-29 | 中国石油化工股份有限公司 | Remaining biochemical sludge decrement treatment system and processing method |
| CN108911478A (en) * | 2018-07-12 | 2018-11-30 | 四川深蓝环保科技有限公司 | A kind of two stages sludge water thermal reaction apparatus |
| CN109355443B (en) * | 2018-12-04 | 2020-07-17 | 浙江华康药业股份有限公司 | System and method for preparing xylose liquid by continuous hydrolysis of hemicellulose |
| CN114558879A (en) * | 2022-03-29 | 2022-05-31 | 北京洁绿环境科技股份有限公司 | Kitchen waste pyrohydrolysis device and method |
| CN114804934A (en) * | 2022-05-25 | 2022-07-29 | 沈阳金利洁环保科技股份有限公司 | Special hydrolysis equipment and process for organic matter treatment |
| CN115181582B (en) * | 2022-07-07 | 2023-06-16 | 华北电力大学（保定） | Two-stage hydrothermal liquefaction waste heat utilization system and method |
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